Catalytic hydrogenation of fluoroolefins, alhpa-alumina supported palladium compositions and their use as hydrogenation catalysts

ABSTRACT

A hydrogenation process is disclosed. The process involves reacting a fluoroolefin with H2 in a reaction zone in the presence of a palladium catalyst to produce a hydrofluoroalkane product, wherein the palladium catalyst comprises palladium supported on a carrier wherein the palladium concentration is from about 0.001 wt % to about 0.2 wt % based on the total weight of the palladium and the carrier. Also disclosed is a palladium catalyst composition consisting essentially of palladium supported on α-Al2O3 wherein the palladium concentration is from about 0.001 wt % to about 0.2 wt % based on the total weight of the palladium and the α-Al2O3. Also disclosed is a hydrogenation process comprising reacting a fluoroolefin with H2 in a reaction zone in the presence of a palladium catalyst to produce a hydrofluoroalkane product, characterized by: the palladium catalyst consisting essentially of palladium supported on α-Al2O3 wherein the palladium concentration is from about 0.001 wt % to about 0.2 wt % based on the total weight of the palladium and the α-Al2O3. Also disclosed is a hydrogenation process comprising (a) passing a mixture comprising fluoroolefin and H2 through a bed of palladium catalyst in a reaction zone wherein the palladium catalyst comprises palladium supported on a carrier; and (b) producing a hydrofluoroalkane product; characterized by: the palladium catalyst in the front of the bed having lower palladium concentration than the palladium catalyst in the back of the bed.

CROSS REFERENCE TO RELATED APPLICATIONS

The present application is a continuation of co-pending U.S. applicationhaving Ser. No. 15/415,960, filed on Jan. 26, 2017, which is adivisional application of U.S. Ser. No. 14/115,661, filed on Nov. 5,2013, now U.S. Pat. No. 9,598,336, which is a ‘371 of internationalapplication having Serial Number PCT/US2012/03822, filed on May 16,2012, which claims benefit of U.S. Ser. No. 61/486,472, filed on May 16,2011, the contents of all of which are incorporated by reference.

BACKGROUND

Field of the Disclosure

This disclosure relates in general to the hydrogenation reactions offluoroolefins with H₂ in the presence of a palladium catalyst supportedon a carrier, compositions of palladium supported on α-Al₂O₃ and theiruse in the fluoroolefin hydrogenation processes.

Description of Related Art

Hydrofluoroalkanes can be employed in a wide range of applications,including their use as refrigerants, solvents, foam expansion agents,cleaning agents, aerosol propellants, dielectrics, fire extinguishantsand power cycle working fluids. For example, HFC-236ea (CF₃CHFCHF₂) canbe used as a heat transfer medium, foam expansion agent, fireextinguishant, et al. Similarly, HFC-245eb (CF₃CHFCH₂F) can be used as aheat transfer medium, foam expansion agent, et al. HFC-236ea andHFC-245eb are also intermediates in the production of HFO-1234yf(CF₃CF═CH₂) which is a refrigerant with zero ozone depletion potentialand low global warming potential.

BRIEF SUMMARY OF THE DISCLOSURE

The present disclosure provides a hydrogenation process. The processcomprises reacting a fluoroolefin with H₂ in a reaction zone in thepresence of a palladium catalyst to produce a hydrofluoroalkane product,wherein said palladium catalyst comprises palladium supported on acarrier wherein the palladium concentration is from about 0.001 wt % toabout 0.2 wt % based on the total weight of the palladium and thecarrier.

The present disclosure also provides a palladium catalyst compositionconsisting essentially of palladium supported on α-Al₂O₃ wherein thepalladium concentration is from about 0.001 wt % to about 0.2 wt % basedon the total weight of the palladium and the α-Al₂O₃.

The present disclosure also provides a hydrogenation process comprisingreacting a fluoroolefin with H₂ in a reaction zone in the presence of apalladium catalyst to produce a hydrofluoroalkane product, characterizedby: said palladium catalyst consisting essentially of palladiumsupported on α-Al₂O₃ wherein the palladium concentration is from about0.001 wt % to about 0.2 wt % based on the total weight of the palladiumand the α-Al₂O₃.

The present disclosure also provides a hydrogenation process comprising(a) passing a mixture comprising fluoroolefin and H₂ through a bed ofpalladium catalyst in a reaction zone wherein the palladium catalystcomprises palladium supported on a carrier; and (b) producing ahydrofluoroalkane product; characterized by: the palladium catalyst inthe front of the bed having lower palladium concentration than thepalladium catalyst in the back of the bed.

DETAILED DESCRIPTION

The hydrogenation reactions of fluoroolefins can be highly exothermic,which can lead to poor temperature control, high levels of undesiredbyproducts, and safety concerns, et al. Some approaches have beenexplored to control the heat. For example, Van Der Puy et al. usedmultiple vapor phase reaction stages as disclosed in U.S. Pat. No.7,560,602. Also disclosed in U.S. Pat. No. 7,560,602 is an approach ofusing 1 wt % Pd/C catalysts diluted with inert protruded packing.However, the multiple-reaction-stage design is costly requiring multiplereactors and heat exchangers. The approach of using high Pd loaded(e.g., 1 wt %) catalysts diluted with inert packing could cause highlylocalized hot spots on the catalyst surface and sintering of highlyvaluable Pd. Thus, there is a need for cost-effective hydrogenationprocesses with good heat control.

The foregoing general description and the following detailed descriptionare exemplary and explanatory only and are not restrictive of theinvention, as defined in the appended claims. Other features andbenefits of any one or more of the embodiments will be apparent from thefollowing detailed description, and from the claims.

As used herein, the terms “comprises,” “comprising,” “includes,”“including,” “has,” “having” or any other variation thereof, areintended to cover a non-exclusive inclusion. For example, a process,method, article, or apparatus that comprises a list of elements is notnecessarily limited to only those elements but may include otherelements not expressly listed or inherent to such process, method,article, or apparatus. Further, unless expressly stated to the contrary,“or” refers to an inclusive or and not to an exclusive or. For example,a condition A or B is satisfied by any one of the following: A is true(or present) and B is false (or not present), A is false (or notpresent) and B is true (or present), and both A and B are true (orpresent).

Also, use of “a” or “an” are employed to describe elements andcomponents described herein. This is done merely for convenience and togive a general sense of the scope of the invention. This descriptionshould be read to include one or at least one and the singular alsoincludes the plural unless it is obvious that it is meant otherwise.

Unless otherwise defined, all technical and scientific terms used hereinhave the same meaning as commonly understood by one of ordinary skill inthe art to which this invention belongs. In case of conflict, thepresent specification, including definitions, will control. Althoughmethods and materials similar or equivalent to those described hereincan be used in the practice or testing of embodiments of the presentinvention, suitable methods and materials are described below. Inaddition, the materials, methods, and examples are illustrative only andnot intended to be limiting.

When an amount, concentration, or other value or parameter is given aseither a range, preferred range or a list of upper preferable valuesand/or lower preferable values, this is to be understood as specificallydisclosing all ranges formed from any pair of any upper range limit orpreferred value and any lower range limit or preferred value, regardlessof whether ranges are separately disclosed. Where a range of numericalvalues is recited herein, unless otherwise stated, the range is intendedto include the endpoints thereof, and all integers and fractions withinthe range.

The term “an elevated temperature”, as used herein, means a temperaturehigher than the room temperature.

The term “hydrogenation”, as used herein, means a process during which apair of hydrogen atoms is added to a double bond in an olefin.

The term “fluoroolefin”, as used herein, means a molecule containingcarbon, fluorine, optionally hydrogen, and at least one carbon-carbondouble bond. Of note are fluoroolefins of the formula C_(n)H_(m)F_(2n-m)wherein n is an integer from 2 to 8 and m is an integer from 0 to 2n−1.In some embodiments of this invention, n is an integer from 2 to 7. Insome embodiments of this invention, the fluoroolefins are terminalfluoroolefins (i.e., the carbon-carbon double bond is at the terminalposition) having 3 to 8 carbons. In some embodiments of this invention,the fluoroolefins are terminal fluoroolefins having 3 to 7 carbons.Exemplary fluoroolefins in this disclosure include CF₃CF═CF₂ (HFP),CF₃CF═CHF (HFO-1225ye), CF₃CH═CF₂, CF₃CF═CH₂, CF₃CH═CHF, CF₃CF═CFCF₃,CF₃CH═CHCF₃, CF₃CH═CFCF₃, CF₃CF₂CF═CFCF₃, CF₃CF₂CH═CHCF₃,(CF₃)₂CFCF═CF₂, CF₃CF═CHC₂F₅, CF₃CH═CFC₂F₅, C₄F₉CH═CH₂,CF₃CF₂CF₂CF₂CF═CFCF₃, CF₃CF₂CF₂CF═CFCF₂CF₃, C₂F₅CH═CFCF₂C₂F₅,C₂F₅CF═CHCF₂C₂F₅, and mixtures thereof.

The term “hydrofluoroalkane”, as used herein, means a saturated moleculecontaining hydrogen, carbon, and fluorine.

Disclosed is a hydrogenation process comprising reacting a fluoroolefinwith H₂ in a reaction zone in the presence of a palladium catalyst toproduce a hydrofluoroalkane product, wherein said palladium catalystcomprises palladium supported on a carrier wherein the palladiumconcentration is from about 0.001 wt % to about 0.2 wt % based on thetotal weight of the palladium and the carrier. In some embodiments ofthis invention, the palladium catalyst consists essentially of palladiumsupported on a carrier wherein the palladium concentration is from about0.001 wt % to about 0.2 wt % based on the total weight of the palladiumand the carrier.

In some embodiments of this invention, the palladium concentration ofthe palladium catalyst is from about 0.001 wt % to about 0.08 wt % basedon the total weight of the palladium and the carrier. In someembodiments of this invention, the palladium concentration of thepalladium catalyst is from about 0.001 wt % to about 0.04 wt % based onthe total weight of the palladium and the carrier. In some embodimentsof this invention, the palladium concentration of the palladium catalystis from about 0.015 wt % to about 0.025 wt % based on the total weightof the palladium and the carrier.

Also disclosed is a palladium catalyst composition consistingessentially of palladium supported on α-Al₂O₃ wherein the palladiumconcentration is from about 0.001 wt % to about 0.2 wt % based on thetotal weight of the palladium and the α-Al₂O₃. Also disclosed is the useof such Pd/α-Al₂O₃ composition as a catalyst in a hydrogenation process.Accordingly, this disclosure also provides a hydrogenation processcomprising reacting a fluoroolefin with H₂ in a reaction zone in thepresence of a palladium catalyst to produce a hydrofluoroalkane product,characterized by: said palladium catalyst consisting essentially ofpalladium supported on α-Al₂O₃ wherein the palladium concentration isfrom about 0.001 wt % to about 0.2 wt % based on the total weight of thepalladium and the α-Al₂O₃.

In some embodiments of this invention, the palladium concentration ofthe Pd/α-Al₂O₃ composition is from about 0.001 wt % to about 0.08 wt %based on the total weight of the palladium and the α-Al₂O₃. In someembodiments of this invention, the palladium concentration of thePd/α-Al₂O₃ composition is from about 0.001 wt % to about 0.04 wt % basedon the total weight of the palladium and the α-Al₂O₃. In someembodiments of this invention, the palladium concentration of thePd/α-Al₂O₃ composition is from about 0.015 wt % to about 0.025 wt %based on the total weight of the palladium and the α-Al₂O₃.

In some embodiments of this invention, the fluoroolefin startingmaterial is C_(n)H_(m)F_(2n-m) and the hydrofluoroalkane product isC_(n)H_(m+2)F_(2n-m), wherein n is an integer from 2 to 8 and m is aninteger from 0 to 2n−1. In some embodiments of this invention, thefluoroolefin starting material is CF₃CF═CF₂ and the hydrofluoroalkaneproduct is CF₃CHFCHF₂. In some embodiments of this invention, thefluoroolefin starting material is CF₃CF═CHF and the hydrofluoroalkaneproduct is CF₃CHFCH₂F. In some embodiments of this invention, thefluoroolefin starting material is a mixture of two or morefluoroolefins. For example, the fluoroolefin starting material can be amixture of CF₃CF═CF₂ and CF₃CF═CHF, and the correspondinghydrofluoroalkane product is a mixture of CF₃CHFCHF₂ and CF₃CHFCH₂F. Foranother example, the fluoroolefin starting material can be a mixture ofCF₃CF═CF₂ and CF₃CF═CFCF₃, and the corresponding hydrofluoroalkaneproduct is a mixture of CF₃CHFCHF₂ and CF₃CHFCHFCF₃. For yet anotherexample, the fluoroolefin starting material can be a mixture ofCF₃CF═CF₂ and CF₃CF═CFC₂F₅, and the corresponding hydrofluoroalkaneproduct is a mixture of CF₃CHFCHF₂ and CF₃CHFCHFC₂F₅. For yet anotherexample, the fluoroolefin starting material can be a mixture ofCF₃CF═CFC₂F₅ and C₂F₅CF═CFCF₂C₂F₅, and the correspondinghydrofluoroalkane product is a mixture of CF₃CHFCHFC₂F₅ andC₂F₅CHFCHFCF₂C₂F₅. For yet another example, the fluoroolefin startingmaterial can be a mixture of CF₃CF═CHC₂F₅ and CF₃CH═CFC₂F₅, and thecorresponding hydrofluoroalkane product is a mixture of CF₃CHFCH₂C₂F₅and CF₃CH₂CHFC₂F₅. For yet another example, the fluoroolefin startingmaterial can be a mixture of CF₃CF═CHF, CF₃CF═CHC₂F₅ and CF₃CH═CFC₂F₅,and the corresponding hydrofluoroalkane product is a mixture ofCF₃CHFCH₂F, CF₃CHFCH₂C₂F₅ and CF₃CH₂CHFC₂F₅. For yet another example,the fluoroolefin starting material can be a mixture of CF₃CF═CHF andCF₃CH═CFCF₃, and the corresponding hydrofluoroalkane product is amixture of CF₃CHFCH₂F and CF₃CH₂CHFCF₃.

Some fluoroolefins in this disclosure, e.g., HFO-1225ye, exist asdifferent configurational isomers or stereoisomers. When the specificisomer is not designated, the present disclosure is intended to includeall configurational isomers, stereoisomers, or any combination thereof.For instance, HFO-1225ye is meant to represent the E-isomer, Z-isomer,or any combination or mixture of both isomers in any ratio.

The hydrogenation reactions between fluoroolefin and H₂ are carried outin the presence of a palladium catalyst. The palladium catalyst in thisdisclosure is a finely divided zero valent palladium metal supported ona carrier. In some embodiments of this invention, the carrier isselected from the group consisting of Al₂O₃, fluorinated Al₂O₃, AlF₃,carbon, Cr₂O₃, SiO₂, TiO₂, ZrO₂ and ZnO.

In some embodiments of this invention, the carrier is carbon. Carbonused in the embodiments of this invention may come from any of thefollowing sources: wood, peat, coal, coconut shells, bones, lignite,petroleum-based residues and sugar. Commercially available carbons whichmay be used include those sold under the following trademarks: Barneby &Sutcliffe™, Darco™, Nucharm, Columbia JXN™, Columbia LCK™, Calgon™ PCB,Calgon™ BPL, Westvaco™, Norit™, Takeda™ and Barnaby Cheny NB™.

The carbon also includes three dimensional matrix porous carbonaceousmaterials. Examples are those described in U.S. Pat. No. 4,978,649. Insome embodiments of the invention, carbon includes three dimensionalmatrix carbonaceous materials which are obtained by introducing gaseousor vaporous carbon-containing compounds (e.g., hydrocarbons) into a massof granules of a carbonaceous material (e.g., carbon black); decomposingthe carbon-containing compounds to deposit carbon on the surface of thegranules; and treating the resulting material with an activator gascomprising steam to provide a porous carbonaceous material. Acarbon-carbon composite material is thus formed.

Carbon includes unwashed and acid-washed carbons. In some embodiments ofthis invention, suitable carbon carrier may be prepared by treating thecarbon with acids such as HNO₃, HCl, HF, H₂SO₄, HClO₄, CH₃COOH, andcombinations thereof. In some embodiments of this invention, acid is HClor HNO₃. Acid treatment is typically sufficient to provide carbon thatcontains less than 1000 ppm of ash. Some suitable acid treatments ofcarbon are described in U.S. Pat. No. 5,136,113. In some embodiments ofthis invention, a carbon carrier is soaked overnight with gentlestirring in a 1 molar solution of the acid prepared in deionized water.The carbon carrier is then separated and washed at least 10 times withdeionized water or until the pH of the washings is about 3. (In someembodiments of this invention, the carbon carrier is then soaked againwith gentle stirring in a 1 molar solution of the acid prepared indeionized water for 12 to 24 hours.) The carbon carrier is then finallywashed with deionized water until the washings are substantially free ofthe anion of the acid (e.g., Cl⁻ or NO₃ ⁻), when tested by standardprocedures. The carbon carrier is then separated and dried at 120° C.The washed carbon is then soaked in 1 molar HF prepared in deionizedwater for 48 hours at room temperature with occasional stirring (e.g.,in a plastic beaker). The carbon carrier is separated and washedrepeatedly with deionized water at 50° C. until the pH of the washingsis greater than 4. The carbon carrier is then dried at 150° C. for 60hours in air followed by calcination at 300° C. for 3 hours in air priorto its use as a carrier.

In some embodiments of this invention, carbon is an activated carbon. Insome embodiments of this invention, carbon is an acid washed activatedcarbon. The carbon can be in the form of powder, granules, or pellets,et al.

In some embodiments of this invention, the carrier is Al₂O₃. Al₂O₃, alsoknown as alumina, exists in several different phases, e.g., α-, γ-, δ-,η-, θ-, and χ-aluminas. In α-Al₂O₃ (corundum), the oxide ions form ahexagonal close-packed structure and the aluminum ions are distributedsymmetrically among the octahedral interstices (see F. A. Cotton and G.Wilkinson, Advanced Inorganic Chemistry, Fifth Edition, John Wiley &Sons, 1988, page 211). γ-Al₂O₃ has a “defect” spinel structure (thestructure of spinel with a deficit of cations). Id. In some embodimentsof this invention, the carrier is α-Al₂O₃. It was surprisingly foundthrough experiments that the hydrogenation processes using α-Al₂O₃ asthe carrier for the palladium catalysts generate fewer byproducts thanother similar hydrogenation processes do when other types of alumina(e.g., γ-Al₂O₃) are used as the carriers.

Alumina may be prepared by methods known in the art. For example, theBayer process is widely used in the industry to produce alumina frombauxite. α-Al₂O₃ can be prepared by heating γ-Al₂O₃ or any hydrous oxideabove 1000° C. Id. γ-Al₂O₃ can be prepared by dehydration of hydrousoxides at about 450° C. Id.

The alumina used in this disclosure can be of any suitable shape anddimensions. For example, alumina can be in the form of powder, granules,spheres, or tablets, et al. Typically, alumina used in this disclosurehas surface area of from about 1 m²/g to about 500 m²/g. In someembodiments of this invention, the alumina has surface area of fromabout 1 m²/g to about 200 m²/g. In some embodiments of this invention,the alumina has surface area of from about 1 m²/g to about 50 m²/g. Insome embodiments of this invention, the alumina has surface area of fromabout 1 m²/g to about 10 m²/g. In some embodiments of this invention,the alumina has surface area of from about 3 m²/g to about 7 m²/g.

Palladium can be deposited on the carrier using techniques known in theart. For example, the palladium catalysts may be prepared byimpregnation methods as generally described by Satterfield on pages93-112 in Heterogeneous Catalysis in Industrial Practice, 2^(nd) edition(McGraw-Hill, New York, 1991). Typically, in an impregnation process, apalladium salt is dissolved in a solvent to form a palladium saltsolution. Examples of suitable palladium salts for this disclosureinclude palladium nitrate, palladium chloride, palladium acetate andpalladium ammine complexes. Examples of suitable solvents include waterand alcohols (e.g., methanol, ethanol, propanol, isopropanol). A carrieris then impregnated with the palladium salt solution. In someembodiments of this invention, a carrier is dipped into an excess amountof the palladium salt solution. In some embodiments of this invention,the incipient wetness technique is used for the impregnation. In anincipient wetness process, a batch of carrier is tumbled and sprayedwith an appropriate amount of the palladium salt solution (the amount ofthe solution is calculated to be just sufficient or slightly less tofill the pores of the carrier). The concentration of the palladium saltsolution may be calculated or adjusted so that the finished catalyst hasthe desired concentration of palladium loaded on the carrier. Theincipient wetness technique is also described by Bailey in U.S. PatentApplication Publication No. 2006/0217579.

The impregnated carrier is then dried, typically at an elevatedtemperature. Optionally, the dried impregnated carrier is calcined. Thecalcination is typically carried out at a temperature of from about 100°C. to about 600° C. In some embodiments of this invention, thecalcination is carried out in the presence of an inert gas (e.g.,nitrogen, argon) and/or oxygen. The resulting catalyst is then typicallytreated with a reducing agent prior to use. In some embodiments of thisinvention, the resulting catalyst is reduced in a flow of hydrogen at anelevated temperature. The hydrogen flow may be diluted with inert gassuch as nitrogen, helium, or argon. The reduction temperature istypically from about 100° C. to about 500° C. In some embodiments ofthis invention, the reduction may be carried out in a liquid phase byhydrazine or formic acid as described by Boitiaux et al. in U.S. Pat.No. 4,533,779.

The hydrogenation process can be carried out in the liquid phase orvapor phase using well-known chemical engineering practice, whichincludes continuous, semi-continuous or batch operations.

In some embodiments of this invention, the hydrogenation process iscarried out in the liquid phase. The liquid phase hydrogenation reactiontemperature is typically from about 0° C. to about 200° C. In someembodiments of this invention, the liquid phase hydrogenation reactiontemperature is from about 25° C. to about 100° C. The pressure of theliquid phase hydrogenation may vary widely from less than 1 atmosphereto 30 atmospheres or more.

Optionally, the liquid phase hydrogenation process is carried out in thepresence of a solvent. The solvent can be polar or non-polar. Suitablepolar solvents include water, alcohols, glycol, acetic acid,dimethylformamide (DMF), N-methylpyrrolidone (NMP), triethylamine, andmixtures thereof. In some embodiments of this invention, the polarsolvent is methanol, ethanol, or mixtures thereof. Suitable non-polarsolvents include inert low dielectric alkanes (e.g., nonane andcyclohexane) and inert low dielectric aromatics (e.g., toluene, benzeneand ortho xylene). In some embodiments of this invention, the solventcan also be the expected hydrofluoroalkane product.

In some embodiments of this invention, the hydrogenation process iscarried out in the vapor phase. The vapor phase hydrogenation reactiontemperature is typically from about room temperature to about 300° C. Insome embodiments of this invention, the vapor phase hydrogenationreaction temperature is from about 50° C. to about 200° C.

The vapor phase hydrogenation process can be conducted atsuperatmospheric, atmospheric, or subatmospheric pressures. In someembodiments of this invention, the vapor phase hydrogenation reactionpressure is from about 10 psig to about 500 psig. In some embodiments ofthis invention, the vapor phase hydrogenation reaction pressure is fromabout 50 psig to about 200 psig.

The vapor phase hydrogenation process of this disclosure may beconducted by methods known in the art. In some embodiments of thisinvention, the fluoroolefin and H₂ starting materials, optionally with adiluent, are co-fed to a reactor containing the palladium catalyst. Insome embodiments of this invention, the fluoroolefin and H₂ startingmaterials, optionally with a diluent, are passed through the palladiumcatalyst bed in a reactor.

In some embodiments of this invention, the vapor phase hydrogenationprocess is conducted without a diluent.

In some embodiments of this invention, the vapor phase hydrogenationprocess is conducted in the presence of a diluent. In some embodimentsof this invention, the diluent is co-fed to the reaction zone with thefluoroolefin and H₂ starting materials. In some embodiments of thisinvention, the molar ratio of the diluent to fluoroolefin startingmaterial co-fed to the reaction zone is from about 100:1 to about 1:1.In some embodiments of this invention, the molar ratio of the diluent tofluoroolefin starting material co-fed to the reaction zone is from about10:1 to about 1:1. In some embodiments of this invention, the molarratio of the diluent to fluoroolefin starting material co-fed to thereaction zone is from about 5:1 to about 1:1. The diluent can be aninert gas which does not react under the hydrogenation conditions ofthis disclosure. In some embodiments of this invention, the diluent isHe, Ar, or N₂. The diluent can also be the expected hydrofluoroalkaneproduct. For example, when fluoroolefin starting material is HFP,HFC-236ea can be used as the diluent to control the reactiontemperature. In some embodiments of this invention, the HFC-236eadiluent is co-fed with HFP and H₂ to the reaction zone. For anotherexample, when fluoroolefin starting material is HFO-1225ye, HFC-245ebcan be used as the diluent to control the reaction temperature. In someembodiments of this invention, the HFC-245eb diluent is co-fed withHFO-1225ye and H₂ to the reaction zone.

In some embodiments of this invention, the diluent is selected from thegroup consisting of saturated hydrocarbons and saturatedhydrofluorocarbons. Suitable saturated hydrocarbons include C1 to C8alkanes such as methane, ethane, propane et al. Suitable saturatedhydrofluorocarbons include C1 to C8 saturated hydrofluorocarbons such asCHF₃, CH₂F₂, CHF₂CF₃, CHF₂CHF₂, CH₂FCF₃, CF₃CF₃, CF₃CF₂CF₃, CF₃CHFCH₂F,CF₃CH₂CHF₂, CF₃CHFCH₃, CF₃CH₂CH₂F, CF₃CHFCHF₂, CF₃CH₂CF₃, CF₃CF₂CH₂F,CF₃CH₂CH₂CF₃, CF₃CHFCHFC₂F₅, C₆F₁₄, and C₂F₅CHFCHFC₃F₇.

The molar ratio of H₂ to fluoroolefin fed to the reaction zone in thevapor phase hydrogenation process can be largely varied. Typically, themolar ratio of H₂ to fluoroolefin fed to the reaction zone in the vaporphase hydrogenation process is from about 0.1:1 to about 100:1. In someembodiments of this invention, the molar ratio is from about 0.5:1 toabout 5:1. In some embodiments of this invention, the molar ratio isfrom about 0.9:1 to about 3:1.

The effluent from the vapor phase hydrogenation reaction zone istypically a product mixture comprising unreacted starting materials,diluent (if used in the process), the desired hydrofluoroalkane productand some byproducts. The desired hydrofluoroalkane product may berecovered from the product mixture by conventional methods. In someembodiments of this invention, the desired hydrofluoroalkane product maybe purified or recovered by distillation. In some embodiments of thisinvention, the unreacted starting materials, and optionally diluent (ifused in the process), are recovered and recycled back to the reactionzone.

Also disclosed is a hydrogenation process comprising (a) passing agaseous or liquid mixture comprising fluoroolefin and H₂ through a bedof palladium catalyst in a reaction zone wherein the palladium catalystcomprises palladium supported on a carrier; and (b) producing ahydrofluoroalkane product; characterized by: the palladium catalyst inthe front of the bed having lower palladium concentration than thepalladium catalyst in the back of the bed. The front of the bed is theflow entrance to the catalyst bed, and the back of the bed is the flowexit from the catalyst bed. In some embodiments of this invention, thepalladium concentration of the catalyst in the front of the bed is fromabout 0.001 wt % to about 0.2 wt % based on the total weight of thepalladium and the carrier, and the palladium concentration of thecatalyst in the back of the bed is from about 0.1 wt % to about 1 wt %based on the total weight of the palladium and the carrier. In someembodiments of this invention, the palladium concentration of thecatalyst in the front of the bed is from about 0.001 wt % to about 0.08wt % based on the total weight of the palladium and the carrier, and thepalladium concentration of the catalyst in the back of the bed is fromabout 0.2 wt % to about 0.8 wt % based on the total weight of thepalladium and the carrier. In some embodiments of this invention, thepalladium concentration of the catalyst in the front of the bed is fromabout 0.001 wt % to about 0.04 wt % based on the total weight of thepalladium and the carrier, and the palladium concentration of thecatalyst in the back of the bed is from about 0.3 wt % to about 0.6 wt %based on the total weight of the palladium and the carrier. In someembodiments of this invention, the palladium concentration of thecatalyst in the front of the bed is from about 0.015 wt % to about 0.025wt % based on the total weight of the palladium and the carrier, and thepalladium concentration of the catalyst in the back of the bed is fromabout 0.3 wt % to about 0.6 wt % based on the total weight of thepalladium and the carrier.

In some embodiments of this invention, the catalyst bed comprises two ormore sections with the same or different lengths wherein each sectioncomprises palladium catalysts having the same palladium concentration.For example, the catalyst bed can comprise a front section and a backsection, wherein the front section comprises palladium catalysts with0.02 wt % palladium concentration and the back section comprisespalladium catalysts with 0.5 wt % palladium concentration, and whereinthe length of the front section is about 60% of the total bed length andthe length of the back section is about 40% of the total bed length. Insome embodiments of this invention, the catalyst bed comprises palladiumcatalysts with continuously increasing palladium concentrations from thefront to the back of the catalyst bed.

The reactors, distillation columns, and their associated feed lines,effluent lines, and associated units used in applying the processes ofembodiments of this invention may be constructed of materials resistantto corrosion. Typical materials of construction include Teflon™ andglass. Typical materials of construction also include stainless steels,in particular of the austenitic type, the well-known high nickel alloys,such as Monel™ nickel-copper alloys, Hastelloy™ nickel-based alloys and,Inconel™ nickel-chromium alloys, and copper-clad steel.

Many aspects and embodiments have been described above and are merelyexemplary and not limiting. After reading this specification, skilledartisans appreciate that other aspects and embodiments are possiblewithout departing from the scope of the invention.

EXAMPLES

The concepts described herein will be further described in the followingexamples, which do not limit the scope of the invention described in theclaims.

LEGEND 245eb is CF₃CHFCH₂F 236ea is CF₃CHFCHF₂ HFP is CF₃CF═CF₂ 254eb isCH₃CHFCF₃ 1225ye is CF₃CF═CHFGeneral Procedure for Examples 1-5

The following general procedure is illustrative of the reactor and thethermocouple layout for the temperature measurement. The hydrogenationreaction was carried out by passing a gaseous mixture through a bed ofpalladium catalyst. 1225ye used herein contained 97-98% Z isomers and2-3% E isomers. Part of the reactor effluent was sampled on-line fororganic product analysis using GC-FID (Gas Chromatograph—FlameIonization Detector).

A vertically oriented Hastelloy™ reactor (1 inch OD, 0.065 inch wall)jacketed by a recirculating hot oil system was used in all theexperiments described below. The reactor was charged with 28.6 cm³palladium catalysts in the form of ⅛ inch spheres or ⅛ inch×⅛ inchtablets. The palladium catalyst bed in the reactor rose to 3 inches inheight and was packed between ⅛ inch Denstone™ α-A₂O₃ spheres (on top)and ¼ inch Hastelloy™ protruded packing (at the bottom).

The gaseous mixture of starting materials and a diluent was pre-heatedand passed through the reactor entering at the top and exiting at thebottom. A ⅛ inch thermocouple situated along the center of the reactormeasured the temperature profile at 8 points: −0.5 inch, 0 inch, 0.5inch, 1 inch, 1.5 inch, 2 inch, 2.5 inch, and 3 inch. The point of “−0.5inch” was about 0.5 inch above the catalyst bed; the point of “0 inch”was at about the top of the catalyst bed; and the point of “0.5 inch”was about 0.5 inch below the top of the catalyst bed; and so on.

Example 1

Example 1 demonstrates that hydrogenation of HFP over 0.1 wt %Pd/α-Al₂O₃ has good control of heat and produces good yields ofHFC-236ea with high selectivity.

A gaseous mixture of HFP, H₂, and 236ea was fed into the reactor. TheHFP flow rate is shown in Table 1. The amount of H₂ or 236ea relative toHFP in the gaseous mixture is also shown in Table 1. Table 1 also showsthe temperature profile in the reactor and the analytical results of thecomposition of the effluent from the reactor.

TABLE 1 (Part A) Feed Rate Reactor Effluent HFP Molar Feed RatiosPressure (mol %) Run (g/h) H₂/HFP 236ea/HFP (psig) HFP 236ea 245eb 1 4542.0 5.0 59 4.8 95.2 0.02 2 454 2.0 5.0 60 6.6 93.3 0.01 3 451 2.0 6.0 607.6 92.4 0.01 4 454 2.0 7.0 61 7.8 92.2 0.01 5 455 3.0 6.0 60 8.0 92.00.01 6 452 4.0 5.0 60 8.0 91.9 0.01 7 454 2.0 6.8 60 8.2 91.7 0.01 8 4522.0 7.0 61 7.6 92.4 0.01 9 454 2.0 7.0 61 6.7 93.2 0.01 10 454 2.0 7.061 6.7 93.3 0.01 11 457 2.0 6.9 60 6.0 93.9 0.01 (Part B) Hot OilInternal Temperatures (° C.) Run (° C.) −0.5″ 0″ 0.5″ 1″ 1.5″ 2″ 2.5″ 3″1 74 80 79 78 78 81 118 159 166 2 65 75 73 72 71 72 96 132 143 3 65 7574 72 71 72 86 110 119 4 65 78 76 74 72 73 83 98 106 5 65 76 74 72 71 7285 106 116 6 65 74 72 71 70 71 88 117 130 7 65 76 75 73 72 72 81 95 1028 74 81 80 79 78 79 91 107 114 9 84 85 85 85 85 87 101 121 130 10 94 9192 92 93 95 110 130 138 11 104 95 97 98 99 102 121 144 152

Example 2

Example 2 demonstrates that hydrogenation of HFP over 0.04 wt %Pd/α-Al₂O₃ has good control of heat and produces good yields ofHFC-236ea with high selectivity.

A gaseous mixture of HFP, H₂, and 236ea was fed into the reactor. TheHFP flow rate is shown in Table 2. The amount of H₂ or 236ea relative toHFP in the gaseous mixture is also shown in Table 2. Table 2 also showsthe temperature profile in the reactor and the analytical results of thecomposition of the effluent from the reactor.

TABLE 2 (Part A) Feed Rate Molar Feed Reactor Effluent HFP RatiosPressure (mol %) Run (g/h) H₂/HFP 236ea/HFP (psig) HFP 236ea 245eb 1 912.0 10.0 125 1.4 98.5 0.03 2 138 2.0 6.6 125 1.5 98.5 0.03 3 228 2.0 3.9125 2.2 97.7 0.04 4 226 1.2 3.0 125 4.4 95.6 0.03 5 226 1.2 5.0 100 6.593.5 0.01 6 227 2.0 5.0 100 5.6 94.4 0.01 7 226 3.0 5.1 100 5.3 94.70.01 8 226 3.0 4.9 100 4.8 95.1 0.01 9 227 3.0 5.0 100 4.3 95.7 0.01 10 226 2.0 5.0 100 7.5 92.5 0.01 (Part B) Hot Oil Internal Temperatures (°C.) Run (° C.) −0.5″ 0″ 0.5″ 1″ 1.5″ 2″ 2.5″ 3″ 1 84 86 97 116 130 134134 131 127 2 85 87 103 132 151 155 154 149 143 3 84 88 110 154 180 185182 174 166 4 84 89 121 172 195 196 189 179 168 5 84 86 95 113 129 138143 145 143 6 84 86 95 115 132 142 147 149 147 7 85 86 95 115 132 143148 150 148 8 94 95 105 127 144 155 159 161 159 9 104 104 116 140 159168 172 172 169 10  114 114 124 144 158 165 167 167 165

Example 3

Example 3 demonstrates that hydrogenation of HFP over 0.02 wt %Pd/α-Al₂O₃ has good control of heat and produces good yields ofHFC-236ea with high selectivity.

A gaseous mixture of HFP, H₂, and 236ea was fed into the reactor. TheHFP flow rate is shown in Table 3. The amount of H₂ or 236ea relative toHFP in the gaseous mixture is also shown in Table 3. Table 3 also showsthe temperature profile in the reactor and the analytical results of thecomposition of the effluent from the reactor.

TABLE 3 (Part A) Feed Rate Molar Feed Reactor Effluent HFP RatiosPressure (mol %) Run (g/h) H₂/HFP 236ea/HFP (psig) HFP 236ea 245eb 1 912.0 9.9 100 6.2% 93.7% 0.02% 2 137 2.0 6.7 99 8.6% 91.4% 0.02% 3 227 3.04.0 100 12.9% 87.0% 0.02% 4 228 3.0 3.0 102 11.9% 88.0% 0.03% 5 135 2.06.8 100 9.1% 90.9% 0.01% 6 226 2.0 4.0 100 13.3% 86.7% 0.01% 7 226 3.03.1 101 14.3% 85.6% 0.02% 8 227 3.0 3.0 125 8.6% 91.3% 0.05% 9 226 3.03.0 125 11.3% 88.7% 0.01% 10 227 1.2 2.9 125 13.7% 86.3% 0.01% 11 2261.2 3.0 125 9.3% 90.7% 0.02% 12 228 1.2 3.0 125 14.9% 85.1% 0.01% 13 2273.0 3.0 125 11.9% 88.1% 0.01% 14 226 1.2 2.0 125 10.8% 89.1% 0.02% 15229 0.5 2.0 125 24.2% 75.7% 0.00% 16 228 1.2 2.2 125 10.9% 89.1% 0.02%17 227 3.0 3.0 125 14.0% 85.9% 0.01% (Part B) Hot Oil InternalTemperatures (° C.) Run (° C.) −0.5″ 0″ 0.5″ 1″ 1.5″ 2″ 2.5″ 3″ 1 84 8588 91 93 96 98 100 2 84 84 85 89 93 96 101 105 108 3 84 85 86 90 96 101110 118 124 4 84 85 86 92 101 111 127 142 152 5 85 84 85 88 91 94 99 103106 6 84 84 85 89 94 99 107 115 121 7 84 85 86 90 97 104 117 130 138 885 94 98 108 123 140 160 173 177 9 94 85 87 94 105 117 135 149 158 10 8594 97 105 117 129 143 153 159 11 94 114 120 137 162 180 193 197 194 12114 84 87 93 102 111 124 133 139 13 84 85 87 93 104 114 130 142 151 1484 85 91 107 136 164 188 194 189 15 85 85 87 94 104 113 123 127 128 1684 85 92 111 142 167 186 189 181 17 84 85 87 93 101 109 120 129 136

Example 4

Example 4 demonstrates that hydrogenation of 1225ye over 0.1 wt %Pd/α-Al₂O₃ has good control of heat and produces good yields ofHFC-245eb with high selectivity.

A gaseous mixture of 1225ye, H₂, and 245eb was fed into the reactor. The1225ye flow rate is shown in Table 4. The amount of H₂ or 245eb relativeto 1225ye in the gaseous mixture is also shown in Table 4. Table 4 alsoshows the temperature profile in the reactor and the analytical resultsof the composition of the effluent from the reactor.

TABLE 4 (Part A) Feed Molar Feed Rate Ratios Reactor Effluent 1225ye H₂/245eb/ Pressure (mol %) Run (g/h) 1225ye 1225ye (psig) 1225ye 254eb245eb 1 91 2.0 9.9 75 1.9 0.17 97.9 2 135 2.0 6.6 75 2.5 0.16 97.4 3 2262.0 4.0 75 2.7 0.18 97.0 4 339 2.0 2.7 75 3.9 0.22 95.8 5 226 1.5 5.9 754.4 0.09 95.4 6 226 2.0 4.0 76 3.0 0.12 96.8 7 227 2.0 4.0 60 3.7 0.1096.2 8 227 2.0 4.0 60 3.6 0.09 96.3 9 227 4.0 2.1 60 2.4 0.16 97.4 10227 3.0 3.0 60 2.7 0.12 97.2 11 227 1.5 6.0 60 5.0 0.09 94.9 12 271 1.24.9 60 6.5 0.09 93.4 13 343 1.2 3.7 60 7.8 0.10 92.1 14 452 1.2 2.6 608.4 0.12 91.5 15 226 2.0 4.0 60 4.0 0.08 95.9 16 92 2.0 9.8 60 2.8 0.0697.1 17 228 2.0 4.0 60 4.3 0.10 95.6 18 227 0.5 4.0 60 11.2 0.09 88.7 19225 2.0 4.0 60 4.4 0.09 95.5 (Part B) Hot Oil Internal Temperatures (°C.) Run (° C.) −0.5″ 0″ 0.5″ 1″ 1.5″ 2″ 2.5″ 3″ 1 85 91 108 121 126 127125 122 2 85 86 94 118 138 145 146 143 138 3 85 87 100 139 172 182 181175 167 4 84 87 102 156 202 215 215 208 197 5 84 82 86 102 122 134 140144 143 6 85 87 97 132 166 178 180 175 167 7 85 87 97 130 163 176 178174 166 8 85 77 86 118 152 167 169 166 158 9 75 77 95 155 195 196 184167 152 10 75 77 90 135 175 185 181 172 160 11 75 77 80 93 111 123 130134 132 12 75 77 81 97 119 133 140 144 142 13 75 77 82 102 132 150 159163 160 14 75 77 86 119 166 189 198 199 193 15 75 77 84 112 147 164 168166 159 16 75 76 79 88 99 106 109 111 109 17 75 77 83 106 140 159 166166 160 18 75 78 83 99 117 124 124 122 117 19 75 77 84 109 144 162 167166 159

Example 5

Example 5 demonstrates that hydrogenation of 1225ye over 0.02 wt %Pd/α-Al₂O₃ has good control of heat and produces good yields ofHFC-245eb with high selectivity.

A gaseous mixture of 1225ye, H₂, and 245eb was fed into the reactor. The1225ye flow rate is shown in Table 5. The amount of H₂ or 245eb relativeto 1225ye in the gaseous mixture is also shown in Table 5. Table 5 alsoshows the temperature profile in the reactor and the analytical resultsof the composition of the effluent from the reactor.

TABLE 5 (Part A) Feed Molar Feed Rate Ratios Reactor Effluent 1225ye H₂/245eb/ Pressure (mol %) Run (g/h) 1225ye 1225ye (psig) 1225ye 254eb245eb 1 92 1.9 9.8 75 5.0% 0.10% 94.9% 2 138 2.0 6.6 75 6.9% 0.08% 93.0%3 228 2.0 3.9 75 10.4% 0.09% 89.5% 4 227 3.0 2.9 74 10.7% 0.12% 89.1% 5228 3.0 2.9 75 10.7% 0.11% 89.2% 6 226 3.0 3.0 75 9.9% 0.09% 89.9% 7 2283.0 3.0 75 9.7% 0.09% 90.2% 8 227 3.0 3.0 75 9.4% 0.08% 90.5% 9 226 3.03.0 75 11.8% 0.06% 88.2% 10 228 3.0 3.0 77 9.9% 0.07% 90.0% 11 226 4.02.0 75 9.2% 0.10% 90.6% 12 114 2.5 7.6 75 4.7% 0.11% 95.2% 13 222 1.32.9 75 11.2% 0.02% 88.7% 14 114 1.2 5.6 75 9.1% 0.03% 90.8% 15 225 1.23.0 75 12.7% 0.03% 87.3% 16 226 2.0 3.0 75 10.8% 0.04% 89.1% 17 226 4.03.0 75 9.9% 0.04% 90.0% 18 227 5.9 3.0 75 9.9% 0.05% 90.0% 19 225 3.03.0 75 12.5% 0.04% 87.4% (Part B) Hot Oil Internal Temperatures (° C.)Run (° C.) −0.5″ 0″ 0.5″ 1″ 1.5″ 2″ 2.5″ 3″ 1 85 85 87 91 97 100 104 103103 2 84 85 87 93 101 106 112 111 110 3 84 85 88 97 111 119 128 127 1254 84 85 90 104 124 135 142 139 140 5 94 95 100 117 137 147 151 148 151 6104 104 110 128 148 157 160 157 160 7 114 114 120 142 163 171 172 168173 8 124 123 131 154 176 183 183 179 185 9 85 85 90 105 123 131 137 135136 10 104 104 110 130 152 160 164 161 164 11 104 105 114 146 176 181175 168 180 12 104 107 127 161 170 162 144 137 154 13 104 103 105 111118 122 127 127 125 14 104 104 109 118 128 131 132 130 132 15 104 104109 124 141 147 151 149 150 16 104 104 110 129 151 159 164 161 164 17104 104 109 127 149 158 164 161 163 18 104 104 109 125 147 157 162 159162 19 84 85 88 99 116 125 136 135 132General Procedure for Examples 6-7

The following general procedure is illustrative of the reactor and thethermocouple layout for the temperature measurement. The hydrogenationreaction was carried out by passing a gaseous mixture through a bed ofpalladium catalyst. Part of the reactor effluent was sampled on-line fororganic product analysis using GC-FID (Gas Chromatograph—FlameIonization Detector).

An Inconel™ reactor (⅝ inch OD, 0.034 inch wall) jacketed by an aluminumsleeve was used in all the experiments described below. The sleeve washeated by a 5 inch long heater band furnace. The reactor was chargedwith 5 cm³ palladium catalysts in the form of ⅛ inch spheres or ⅛ inch×⅛inch tablets.

The gaseous mixture of HFP, H₂, and N₂ was pre-heated to 50° C. andpassed through the reactor in the direction of from the top of thecatalyst bed to the bottom. The furnace temperature was controlled by athermocouple inside the aluminum sleeve. A 1/16 inch thermocouplesituated along the center of the reactor measured the temperatureprofile at about the top of the catalyst bed (0″ point) and about 1 inchbelow the top (1″ point).

Example 6

Example 6 demonstrates that hydrogenation of HFP over 0.3 wt %Pd/γ-Al₂O₃ generates considerable amount of 245eb byproduct.

A gaseous mixture of HFP, H₂, and N₂ was fed into the reactor. The HFPflow rate is shown in Table 6. The amount of H₂ or N₂ relative to HFP inthe gaseous mixture is also shown in Table 6. Table 6 also shows thetemperature profile in the reactor and the analytical results of thecomposition of the effluent from the reactor.

TABLE 6 Internal Feed Rate Molar Feed Temperatures Reactor Effluent HFPRatios Furnace (° C.) (mol %) Run (sccm) H₂/HFP N₂/HFP (° C.) 0″ 1″ HFP236ea 245eb 1 10 1 10 49 80 52 11.9 85.7 2.0 2 10 5 10 50 75 51 0.1 99.00.9 3 10 1 30 51 84 59 13.1 83.4 2.8 4 5 1 60 51 84 59 10.9 85.5 2.9 510 1 30 70 101 76 13.7 82.5 3.0 6 4.9 2 61 69 86 74 1.9 95.9 1.9 7 4.8 161 70 87 75 9.5 87.4 2.5

Example 7

Example 7 demonstrates that hydrogenation of HFP over 0.3 wt %Pd/α-Al₂O₃ does not generate 245eb byproduct.

A gaseous mixture of HFP, H₂, and N₂ was fed into the reactor. The HFPflow rate is shown in Table 7. The amount of H₂ or N₂ relative to HFP inthe gaseous mixture is also shown in Table 7. Table 7 also shows thetemperature profile in the reactor and the analytical results of thecomposition of the effluent from the reactor.

TABLE 7 Internal Feed Molar Feed Temperatures Reactor Effluent RateRatios Furnace (° C.) (mol %) Run HFP (sccm) H₂/HFP N₂/HFP (° C.) 0″ 1″HFP 236ea 245eb 1 10 1 30 49 56 55 49.27 50.47 0.00 2 10 5 30 48 62 558.67 91.13 0.00 3 10 2.5 30 51 64 59 19.20 80.54 0.00 4 20 2.5 15 47 7762 14.91 84.83 0.00

Note that not all of the activities described above in the generaldescription or the examples are required, that a portion of a specificactivity may not be required, and that one or more further activitiesmay be performed in addition to those described. Still further, theorder in which activities are listed are not necessarily the order inwhich they are performed.

In the foregoing specification, the concepts have been described withreference to specific embodiments. However, one of ordinary skill in theart appreciates that various modifications and changes can be madewithout departing from the scope of the invention as set forth in theclaims below. Accordingly, the specification is to be regarded in anillustrative rather than a restrictive sense, and all such modificationsare intended to be included within the scope of invention.

Benefits, other advantages, and solutions to problems have beendescribed above with regard to specific embodiments. However, thebenefits, advantages, solutions to problems, and any feature(s) that maycause any benefit, advantage, or solution to occur or become morepronounced are not to be construed as a critical, required, or essentialfeature of any or all the claims.

It is to be appreciated that certain features are, for clarity,described herein in the context of separate embodiments, may also beprovided in combination in a single embodiment. Conversely, variousfeatures that are, for brevity, described in the context of a singleembodiment, may also be provided separately or in any subcombination.

What is claimed is:
 1. A composition comprising at least onefluoroolefin having the formula C_(n)-H_(m)F_(2n−m); in; a at least onehydrofluoralkane having the formula C_(n)H_(m+2) F_(2n−m), wherein n isan integer from 2 to 8 and m is an integer from 0 to 2n−1, and apalladium catalyst comprising palladium supported on a carriercomprising α-Al₂O₃, wherein the palladium concentration is from about0.001 wt % to about 0.08 wt % based on the total weight of the palladiumand the carrier, wherein the molar ratio of the hydrofluoroalkane to thefluoroolefin ranges from about 10:1 to about 1:1.
 2. The composition ofclaim 1 wherein the palladium concentration of the palladium catalyst isfrom about 0.001 wt % to about 0.04 wt % based on the total weight ofthe palladium and the carrier.
 3. The composition of claim 1 wherein thepalladium concentration of the palladium catalyst is from about 0.015 wt% to about 0.025 wt % based on the total weight of the palladium and thecarrier.
 4. The composition of claim 1 wherein the fluoroolefin isselected from the group consisting of CF₃CF═CF₂ (HFP), CF₃CF═CHF(HFO-1225ye), CF₃CH═CF₂, CF₃CF═CH₂, CF₃CH═CHF, CF₃CF═CFCF₃, CF₃CH═CHCF₃,CF₃CH═CFCF₃, CF₃CF₂CF═CF₃, CF₃CF₂CH═CHCF₃, (CF₃)₂CFCF═CF₂, CF₃CF═CHC₂F₅,CF₃CH═CFC₂F₅, C₄F₉CH═CH₂, CF₃CF₂CF₂CF₂CF═CFCF₃, CF₃CF₂CF₂CF═CFCF₂CF₃,C₂F₅CH═CFCF₂C₂F₅, C₂F₅CF═CHCF₂C₂F₅, and mixtures thereof.
 5. Thecomposition of claim 1 wherein the molar ratio of the hydrofluoroalkaneto fluoroolefin is from 5:1 to 1:1.
 6. The composition of claim 1wherein the fluoroolefin is CF₃CF═CF₂ and the hydrofluoroalkane isCF₃CHFCHF₂ or where the fluoroolefin is CF₃CF═CHF and thehydrofluoroalkane is CF₃CHFCH₂F.
 7. The composition of claim 1 wherehydrogen is additionally present.
 8. The composition of claim 7 whereinthe molar ratio of hydrogen to fluoroolefin is from 0.5:1 to 5:1.
 9. Acomposition comprising a fluoroolefin having the formulaC_(n)-H_(m)F_(2·m); a hydrofluoroalkane which is the hydrogenationproduct of said fluoroolefin, said hydrofluoralkane having the formulaC_(n)H_(m+2)F_(2n−m), wherein n is an integer from 2 to 8 and m is aninteger from 0 to 2n−1, a bed of palladium catalyst supported on acarrier comprising α-Al₂O₃, the bed of palladium catalyst having a frontand a back, wherein the palladium catalyst in the front of the bed has alower palladium concentration than the palladium catalyst in the back ofthe bed, wherein the palladium concentration of the catalyst in thefront of the bed is from about 0.001 wt % to about 0.08 wt % based onthe total weight of the palladium and the carrier, and the palladiumconcentration of the catalyst in the back of the bed is from about 0.1wt % to about 1 wt % based on the total weight of the palladium and thecarrier.
 10. The composition according to claim 9 wherein the palladiumconcentration of the catalyst in the front of the bed is from about0.001 wt % to about 0.08 wt % based on the total weight of the palladiumand the carrier, and the palladium concentration of the catalyst in theback of the bed is from about 0.2 wt % to about 0.8 wt % based on thetotal weight of the palladium and the carrier.
 11. The compositionaccording to claim 9 wherein the palladium concentration of the catalystin the front of the bed is from about 0.001 wt % to about 0.04 wt %based on the total weight of the palladium and the carrier, and thepalladium concentration of the catalyst in the back of the bed is fromabout 0.3 wt % to about 0.6 wt % based on the total weight of thepalladium and the carrier.
 12. The composition according to claim 9wherein the palladium concentration of the catalyst in the front of thebed is from about 0.015 wt % to about 0.025 wt % based on the totalweight of the palladium and the carrier, and the palladium concentrationof the catalyst in the back of the bed is from about 0.3 wt % to about0.6 wt % based on the total weight of the palladium and the carrier. 13.The composition of claim 9 wherein the fluoroolefin is selected from thegroup consisting of CF₃CF═CF₂ (HFP), CF₃CF═CHF (HFO-1225ye), CF₃CH═CF₂,CF₃CF═CH₂, CF₃CH═CHF, CF₃CF═CFCF₃, CF₃CH═CHCF₃, CF₃CH═CFCF₃,CF₃CF₂CF═CFCF₃, CF₃CF₂CH═CHCF₃, (CF₃)₂CFCF═CF₂, CF₃CF═CHC₂F₅,CF₃CH═CFC₂F₅, C₄F₉CH═CH₂, CF₃CF₂CF₂CF₂CF═CFCF₃, CF₃CF₂CF₂CF═CFCF₂CF₃,C₂F₅CH═CFCF₂C₂F₅, C₂F₅CF═CHCF₂C₂F₅, and mixtures thereof.
 14. Thecomposition of claim 9 wherein the molar ratio of the hydrofluoroalkaneto fluoroolefin is from 5:1 to 1:1 at the back of the bed.
 15. Thecomposition of claim 9 wherein the fluoroolefin is CF₃CF═CF₂ and thehydrofluoroalkane is CF₃CHFCHF₂ or where the fluoroolefin is CF₃CF═CHFand the hydrofluoroalkane is CF₃CHFCH₂F.
 16. The composition of claim 9where H₂ is additionally present and the molar ratio of H₂ tofluoroolefin ranges from about 0.5:1 to about 5:1.